US7288690B2 - Method and apparatus for steam cracking hydrocarbons - Google Patents

Method and apparatus for steam cracking hydrocarbons Download PDF

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US7288690B2
US7288690B2 US11/254,561 US25456105A US7288690B2 US 7288690 B2 US7288690 B2 US 7288690B2 US 25456105 A US25456105 A US 25456105A US 7288690 B2 US7288690 B2 US 7288690B2
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fuel
combustion
mixture
cracking
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US20060116543A1 (en
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Serge Bellet
Jean Pinon
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BP Chemicals Ltd
Ineos Sales UK Ltd
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BP Chemicals Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/023—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only thermal cracking steps
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/24—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/14—Combined heat and power generation [CHP]

Definitions

  • the present invention relates to a method of steam cracking hydrocarbons in order to produce olefins, in particular.
  • a known steam cracking method consists in causing a mixture of hydrocarbons and steam to pass along at least one cracking tube such as a coil placed in a furnace.
  • the hydrocarbons On being raised to high temperature, e.g. in the range 700° C. to 900° C., the hydrocarbons are cracked so as to provide olefins in particular and possibly also diolefins and light alkanes such as methane.
  • olefins in particular and possibly also diolefins and light alkanes such as methane.
  • a steam cracking furnace uses radiant heat delivered by burners such as conventional gas or oil burners as its source of heat.
  • the burners are often placed on the floor and/or the walls of the furnace and they define a high temperature zone in the furnace, also referred to as the “radiation” zone of the furnace.
  • a convection zone through which the hot combustion gases escape from the radiation zone, which convection zone is generally used for preheating the mixture of hydrocarbons to be cracked, also known as the “feedstock” to be cracked.
  • the mixture is usually preheated to about 500° C. in the convection zone of a furnace, after which it enters the radiation zone of the furnace where it reaches the reaction temperature, in particular a temperature in the range 700° C. to 900° C.
  • Such a method thus consists in performing an entire heat treatment program from the preheating stage to the cracking stage proper within a single heating furnace, using the radiant heat from the burners as the source of heat.
  • the furnace must be capable of withstanding the highest temperatures involved in the method, and it must also be a piece of equipment that is large in size, with all of the manifest drawbacks associated with size.
  • the method of steam cracking also requires accurate control over heating in the reaction zone, i.e. the high temperature zone.
  • temperature can only be controlled indirectly, and thus inaccurately.
  • U.S. Pat. No. 4,912,282 describes a method and apparatus for steam cracking hydrocarbons to produce olefins such as ethylene.
  • the apparatus comprises a cracking furnace that is heated by burning fuel using an oxidizer comprising a mixture of air and exhaust gas from a gas turbine that forms part of a cogenerator system.
  • the gas turbine is coupled to an electricity generator which feeds electricity to compressors and pumps.
  • the combustion air as preheated in that method enables the combustion temperature to be increased and thus enables the efficiency of the radiation zone (high temperature zone) of the cracking furnace to be increased, and consequently enables fuel consumption to be reduced. Nevertheless, temperature control in the radiation zone of the cracking furnace remains inaccurate, and the size of the furnace is very large. Furthermore, a high level of harm continues to be done to the environment by nitrogen oxide being rejected to the atmosphere together with the combustion gases from the cracking furnace.
  • European patent application No. EP 0 806 467 describes a method of pyrolyzing hydrocarbons which is performed together with a continuous decoking method specifically for the purpose of reducing or eliminating the losses of time usually associated with stops for decoking.
  • the pyrolysis method includes a prior step of steam cracking in a steam cracking furnace followed by the pyrolysis step proper which is performed in a pyrolysis reactor at very high temperature and which is intended to produce acetylene hydrocarbons such as acetylene.
  • the steam cracking furnace is normally heated by conventional gas burners, e.g. of the radiant burner type, and that the pyrolysis reactor can be heated either by electrical resistances or by jackets containing gas burners.
  • electrical resistances being powered electrically by a cogenerator system.
  • electrical heating is not at all to be recommended for such a reactor because of high investment and running costs.
  • Japanese patent application JP 09 235 564 proposes a method of thermally cracking hydrocarbons to produce ethylene.
  • the feedstock is preheated by means of the combustion heat from a preheating furnace provided with conventional burners, and is then subjected to thermal cracking in a high temperature zone by means of induction heating.
  • the electricity required for the induction heating does not come from a cogenerator system.
  • the preheating furnace is provided with conventional burners with all of the above-mentioned drawbacks for that type of heating associated in particular with environmental problems such as rejecting nitrogen oxides to the atmosphere together with the combustion gases of such a furnace.
  • the present invention relates to a method of steam cracking hydrocarbons that makes it possible to avoid or reduce very significantly the drawbacks mentioned above.
  • the invention provides a method of steam cracking hydrocarbons, which method consists in heating a mixture of hydrocarbons and steam to a desired temperature that is high enough to crack the hydrocarbons and transform them into olefins, the method being characterized in that the source of energy needed for heating the mixture is supplied essentially by cogeneration using combustion of a fuel to produce simultaneously both heat energy and mechanical work which is transformed into electricity by an alternator or an electricity generator, and in that the mixture is initially subjected to preheating using the heat energy supplied by the cogeneration, and is subsequently heated to the desired cracking temperature by means of electrical heating using the electricity supplied by the cogeneration.
  • FIG. 1 is a diagram of apparatus for implementing the method of the present invention.
  • the steam cracking method of the present invention is particularly advantageous when the cogeneration uses fuel selected from at least one of the cracked hydrocarbons (i.e. as obtained by the cracking), in particular one or more gaseous alkanes e.g. in the range C 1 to C 4 , and preferably methane.
  • the fuel is preferably a gaseous hydrocarbon fuel.
  • a preferably gaseous fuel for combustion purposes enables cogeneration to produce simultaneously both heat and mechanical work.
  • the mechanical work as produced by a heat engine or a gas engine, for example, or preferably by a gas turbine, is generally used to drive at least one alternator that produces electricity.
  • cogeneration thus provides both heat and mechanical work which can be reused in appropriate and advantageous manner.
  • cogeneration implemented in the present invention advantageously gives self-contained control and management over the production of electricity adapted to the specific requirements of the electrical heating, e.g. by selecting the power and/or the frequency of the electricity to be suitable for achieving the desired high temperatures for cracking.
  • cogeneration which preferably uses a gaseous fuel such as natural gas or preferably one or more of the hydrocarbons produced by the cracking, e.g. alkanes in the range C 1 to C 4 and in particular methane, has the advantage of providing not only significant energy savings, but also a solution to concerns related to combating atmospherical pollution, in particular by minimizing the amount of nitrogen oxides that are rejected into the atmosphere together with the combustion gases.
  • the method of the present invention presents enormous potential associated with accurate control over the temperature profile in the electrical heating zone where the hydrocarbons are cracked. It provides greater flexibility in selection of the temperature profile, thus making it possible to optimize the cracking of hydrocarbons.
  • the method of the present invention advantageously presents implementation that is much simpler than that required for previously known steam cracking methods. It also has the enormous advantage of being economically viable.
  • Cogeneration in particular by means of a gas turbine generally comprises: a) compressing fresh air or oxidizer (containing oxygen) to an absolute pressure of 1.5 megapascals (MPa) to 2.5 MPa, for example, depending on the desired electrical power; then b) introducing the air or oxidizer as compressed in this way and as mixed with the preferably gaseous fuel into a combustion chamber to perform combustion; then c) after combustion, expanding the hot combustion gases in a turbine that is generally coupled to at least one generator or alternator producing electricity; and d) recovering the hot combustion gases as a source of heat.
  • a portion of the mechanical work that is produced can be used for the initial compression of air or oxidizer, e.g. by driving an air turbocompressor.
  • the temperature of the hot combustion gases delivered by the cogeneration (after expansion) can lie in the range 400° C. to 570° C., and preferably in the range 470° C. to 550° C.
  • This heat energy is preferably used directly to preheat the mixture for cracking.
  • the hot combustion gases exchange their heat with the mixture for cracking which can flow as a countercurrent to said hot gases, for example, passing through one or more preheating zones so as to be heated up to a temperature of about 500° C., for example.
  • the hot combustion gases leaving the cogeneration can be relatively rich in oxygen, for example they can contain 10% to 18% and preferably 12% to 17% by volume of oxygen. It is possible to use part of this oxygen as an oxidizer, thereby performing post-combustion and increasing the heat energy used for preheating the mixture that is to be cracked. In practice, post-combustion can be performed directly at the outlet of the cogeneration prior to preheating the mixture for cracking. Under such circumstances, the hot combustion gases leaving cogeneration are introduced into a post-combustion chamber, and a fuel, which can be different from but is preferably identical to that used for the cogeneration, is added thereto so as to come into contact with the hot gases.
  • the fuel used in the post-combustion is preferably one or more hydrocarbons produced by the cracking, for example alkanes in the range C 1 to C 4 , and in particular methane.
  • alkanes in the range C 1 to C 4
  • methane methane
  • the temperature reached by the post-combustion exhaust gases can lie in the range 500° C. to 1100° C., and preferably in the range 550° C. to 800° C., e.g. 700° C.
  • These gases can then be used directly to preheat the mixture for cracking. Under such circumstances, they exchange heat with the mixture for cracking which flows as a countercurrent to said exhaust gases, for example, by passing in succession through one or more preheating and superheating zones. It is also possible, optionally, to exchange the heat of these exhaust gases simultaneously with water or steam in one or more boilers so as to produce the hot water or the steam at low or medium pressure (e.g. 0.1 MPa to 12 MPa) and increase the energy efficiency of the method.
  • the steam produced in this way can be used in situ as a source of energy in the steam cracking method and in particular during the steps of separating, fractioning, and purifying the olefins and light alkanes that are produced.
  • the oxygen content of the post-combustion exhaust gas can lie in the range 1% to 10% and preferably in the range 1% to 5%, by volume.
  • the temperature of the post-combustion exhaust gas after heat exchange with the mixture for cracking is substantially decreased and can lie in the range 120° C. to 300° C., and preferably in the range 150° C. to 250° C.
  • the mixture of hydrocarbons and of steam can thus be preheated by passing through one or more preheating and possibly superheating zones, essentially by convection in heat exchangers exchanging heat with the combustion of gas from the cogeneration or preferably the exhaust gas from post-combustion as described above.
  • the temperature of the mixture after preheating can reach 400° C. to 600° C., and preferably lies in the range 450° C. to 550° C.
  • a cogenerator system constituted by a “Frame 9”® type gas turbine from General Electric capable of delivering 120 megawatts (MW) of electrical power.
  • the heat power which can be produced downstream from that system is 130 MW, and it can be raised up to 150 MW if post-combustion of the kind described above is implemented.
  • the cogenerator system has the energy capacity to run steam cracking furnaces with a total capacity of 300,000 (metric) tonnes per annum of ethylene.
  • the preheated mixture is then heated to the cracking temperature by means of electrical heating powered with the electricity produced by the cogeneration.
  • One of the advantages of the present invention is to be able to adapt at will the amount of electricity provided on site by the cogeneration, and in particular to adapt the electrical power and/or frequency to the specific requirements of the electrical heating, and thus reach the desired cracking temperature throughout the cracking tube(s), in particular in application of a determined temperature-increase profile up to the desired maximum cracking temperature.
  • the electrical heating techniques used for reaching the desired cracking temperature can be induction heating or Joule effect heating, e.g. by means of a resistance element tube.
  • the mixture for cracking can be heated in a heating furnace by induction.
  • the furnace can comprise a plurality of induction heater tubes that are connected together in parallel.
  • the preheated mixture of hydrocarbons and steam flows inside the tubes where it is subjected to thermal cracking suitable for forming olefins, and this is done in said high temperature range obtained by means of the induction furnace.
  • the induction heating tubes can be inside an enclosure which is closed and leaktight.
  • Each induction heating tube can comprise a tube (or “cracking” tube) carrying a flow of the preheated mixture of hydrocarbons and steam, together with an inductor coil wound around the tube. Lagging can be placed between the tube and the coil and further lagging can be placed over the coil as an outer covering.
  • the coil can be constituted by a winding of copper wire.
  • a generator or alternator e.g. operating at high frequency, can be connected to the ends of the coil so as to power the coil electrically, e.g. at high frequency.
  • the generator or alternator can be part of the cogeneration and can deliver exactly the amount of electricity required for induction heating.
  • the generator or the alternator can also be connected to a frequency and power adapter delivering electricity suitable for induction heating of the tube(s) in which the steam cracking reaction is performed.
  • Induction heating is preferably performed at high frequency (HF), in particular at frequencies lying in the range 3 megahertz (MHz) to 30 MHz, e.g. frequencies of 13 MHz and 27 MHz.
  • Induction heating is not limited to HF induction: it is also possible to use intermediate frequencies in the range 1 kilohertz (kHz) to 3 MHz, e.g. 2000 hertz (Hz), or a commercial induction frequency in the range 50 Hz to 100 Hz, e.g. 50 Hz or 60 Hz.
  • the mixture for cracking can be heated in one or more resistance element tubes, by applying electrical voltage between the ends of said tubes carrying the mixture.
  • the heater device based on resistance element tubes comprises one or more tubes in which the mixture of hydrocarbons and steam flows, said tubes being made out of a conductive material, e.g. stainless steel, and said tubes being connected to a voltage generator.
  • the tubes thus act to perform the following functions simultaneously: transport; electrical resistance elements; and heat exchanger surface.
  • the electrical voltage applied to the resistance element tube(s) can be generated by a low voltage or very low voltage transformer powered by the generator or alternator forming part of the cogenerator system.
  • Heating by means of a resistance element tube is preferably implemented by using electricity at a voltage of less than 50 volts (V), thus ensuring safety for personnel.
  • a power modulator can advantageously be used to control the temperature of the mixture of hydrocarbons and steam.
  • ultrasound waves can be applied to the mixture of hydrocarbons and steam during cracking, as described in U.S. Pat. No. 3,819,740. It is possible to use an ultrasound wave generator powered using the electricity provided by the cogeneration.
  • the frequency of the ultrasound waves supplied to the mixture for cracking in the electrical heater apparatus can lie in the range 1 kHz to 800 kHz, e.g. being 10 kHz or 20 kHz. It has been found that applying ultrasound waves during steam cracking of the hydrocarbon mixture serves to avoid or at least reduce internal coking of the cracking tubes and also serves to improve the selectivity of the steam cracking reaction.
  • the mixture of hydrocarbons and steam is subjected to a cracking temperature which can generally begin at an inlet temperature to the electrical heater apparatus lying in the range 400° C. to 700° C., preferably in the range 450° C. to 660° C., and which can generally end at a maximum or outlet temperature from said apparatus lying in the range 700° C. to 900° C., and preferably in the range 760° C. to 850° C.
  • the cracking temperature can increase along the cracking tubes in application of a profile that is continuous or discontinuous as described in European patents Nos. EP 0 252 355 and EP 0 252 356.
  • the mean transit time of the mixture of hydrocarbons and steam between the inlet and the outlet of the electrical heating apparatus can lie in the range 300 milliseconds (ms) to 1800 ms.
  • the reaction volume can be constant or varying all along the cracking tubes between the inlet and the outlet of the electrical heater apparatus, as described in the two above-cited European patents.
  • the present invention also provides hydrocarbon steam cracking apparatus comprising:
  • a cogenerator system comprising a gas turbine ( 1 ) connected to a line ( 2 ) for supplying it with air or oxidizer, to a line ( 3 ) for feeding it with fuel, and to at least one exhaust line ( 9 ) for exhausting hot combustion gases from the gas turbine ( 1 ), the turbine itself being coupled to at least one alternator or electricity generator ( 4 ) connected to at least one electrical line ( 8 );
  • At least one electrical heater apparatus for heating at least one cracking tube ( 6 ) connected to at least one of the transport and heat exchange lines ( 12 ) leaving the chamber ( 14 ), and at least one drawing-off line ( 16 ) for drawing off cracked hydrocarbons, said electrical heater apparatus being connected to at least one of the electrical lines ( 8 ); and
  • At least one zone ( 17 ) for separating and purifying the cracked hydrocarbons said zone being connected to at least one of the drawing-off lines ( 16 ).
  • the electrical heater apparatus comprises at least one induction heating tube ( 6 ), e.g. having an induction coil ( 15 ) wound around said tube and connected to at least one of the electrical lines ( 8 ).
  • the electrical heating apparatus is a Joule effect heating apparatus, e.g. a resistance element tube comprising, for example, one or more tubes having their ends connected to at least one transformer which is in turn connected to at least one of the electrical lines ( 8 ).
  • the resistance element tube heater device can be constituted in particular by one of those specified above.
  • the steam cracking device can also comprise at least one post-combustion chamber ( 10 ) placed on at least one of the lines ( 9 ) for evacuating the combustion gases from the gas turbine ( 1 ) and fed with a fuel feed line, preferably identical to the above-described line ( 3 ) for feeding the gas turbine, or branching therefrom.
  • the fuel feed line can have one or more burners ( 11 ) at its end situated in the post-combustion chamber ( 10 ).
  • the post-combustion chamber ( 10 ) can be directly connected to at least one of the chambers ( 14 ) for preheating the mixture for cracking, such that the exhaust gases from the chamber ( 10 ) in particular can penetrate directly into at least one of the preheating chambers ( 14 ).
  • the post-combustion chamber ( 10 ) can also be indirectly connected to at least one of the preheating chambers ( 14 ) by being connected initially directly to at least one chamber ( 13 ) for superheating the mixture for cracking as already preheated in the chamber ( 14 ).
  • the superheater chamber ( 13 ) has at least one of the transport and heat exchange lines ( 12 ) coming from one of the preheater chambers ( 14 ) passing therethrough, with said superheater chamber ( 13 ) preferably being directly connected to said preheater chamber.
  • the exhaust gases from the post-combustion chamber ( 10 ) pass initially through at least one superheater chamber ( 13 ) and then through at least one preheater chamber ( 14 ) so that the gases can exchange their heat with the mixture for cracking flowing inside at least one of the transport and heat exchange lines ( 12 ).
  • the steam cracking apparatus comprising at least one separation and purification zone ( 17 ) for the hydrocarbons cracked in the tube ( 6 ) can include at least one line ( 19 ) for drawing off at least one of the cracked hydrocarbons, in particular a light hydrocarbon such as an alkane in the range C 1 to C 4 , and in particular methane.
  • At least one line ( 5 ) for recovering the cracked hydrocarbon(s) can run, for example as a branch connection, from the drawing-off line ( 19 ) and can be connected to at least one of the lines for feeding fuel to the gas turbine ( 1 ) and/or optionally a line for feeding fuel to at least one of the above-described post-combustion chambers ( 10 ).
  • the alternator or electricity generator ( 4 ) can be connected to a frequency and power adapter delivering electricity suitable for induction heating the cracking tube ( 6 ) where the steam cracking reaction is performed. It is also possible to use a high frequency alternator, in particular at a frequency of the kind specified above for induction furnace heating.
  • the alternator or electricity generator ( 4 ) can be connected to a low voltage or very low voltage transformer.
  • the steam cracking device can also comprise a network for recovering low or medium pressure steam (e.g. in the range 5 MPa to 10 MPa) by means of a water feed line passing through at least one of the preheater chambers ( 14 ) so as to preheat the water and create steam by heat exchange with the combustion gases passing through said chamber(s). This can also be done by recovering heat energy by heat exchange between the water previously preheated in this way and the cracked hydrocarbons leaving the electrical heater apparatus via the drawing-off line(s) ( 16 ). Thereafter the steam can be separated from the water and recovered in a steam line.
  • low or medium pressure steam e.g. in the range 5 MPa to 10 MPa
  • the steam can then be heated and even superheated by heat exchange between the steam and the combustion gases passing through at least one of the preheater chambers ( 14 ) and preferably between the steam and the exhaust gas from at least one of the post-combustion chambers ( 10 ) passing through at least one of the superheater chambers ( 13 ).
  • the steam line passes through at least one of the preheater and/or preferably superheater chambers ( 14 , 13 ) so as to form steam at low or medium pressure.
  • FIG. 1 is a diagram of apparatus that can be used to implement the method of the present invention.
  • the cogenerator system comprises a gas turbine ( 1 ) coupled to an alternator ( 4 ).
  • the gas turbine is fed by an air or oxidizer supply line ( 2 ) and by a line ( 3 ) for feeding fuel that is preferably gaseous.
  • the cogenerator alternator ( 4 ) delivers electricity via an electrical line ( 8 ).
  • the hot combustion gases escape from the gas turbine ( 1 ) via an exhaust line ( 19 ).
  • the exhaust line feeds a post-combustion chamber ( 10 ) having burners ( 11 ) themselves fed by a fuel feed line ( 3 ) branching from the line ( 3 ) feeding the gas turbine ( 1 ) with fuel.
  • the hot exhaust gases from the post-combustion chamber ( 10 ) pass successively through a superheater chamber ( 13 ) and a preheater chamber ( 14 ) for exchanging heat with the mixture of hydrocarbons and steam flowing along a transport and heat exchange line ( 12 ) which passes in succession through the preheater and superheater chambers ( 14 and 13 ).
  • the transport and heat exchange line ( 12 ) feeds a plurality of induction heater tubes ( 6 ) connected in parallel, only one of which is shown in FIG. 1 .
  • the induction heater tube comprises a cracking tube in which the mixture for cracking flows, and an induction coil ( 15 ) powered by the electrical line ( 8 ) coming from the alternator ( 4 ).
  • the induction heater tube can be isolated in an enclosure ( 7 ).
  • the mixture of hydrocarbons cracked in the tube ( 6 ) leaves the tube via a drawing-off line ( 16 ), and after being quenched one or more times (not shown in FIG. 1 ) it is subjected to fractioning, separation, and purification in a zone ( 17 ), in particular by being compressed and distilled.
  • This zone serves firstly to isolate olefins such as ethylene and propylene via one or more drawing-off lines ( 18 ) and secondly light alkanes, e.g. in the C 1 to C 4 range, and preferably methane, via at least one other drawing-off line ( 19 ).
  • This line has a cracked hydrocarbon recovery line ( 5 ) running therefrom to feed the gas turbine ( 1 ) and/or optionally the post-combustion chamber ( 10 ) with fuel via one of the feed lines ( 3 ).
  • the gaseous fuel feeding the gas turbine ( 1 ) e.g. via the feed line ( 3 ) is preferably at a minimum absolute pressure of 1.5 MPa to 2.0 MPa, e.g. at an absolute pressure lying in the range 1.5 MPa to 5 MPa, and preferably in the range 2 MPa to 4 MPa.
  • the gaseous fuel feeding the post-combustion chamber ( 10 ), e.g. via the feed line ( 3 ), can be at a pressure which is lower than that of the fuel feeding the gas turbine ( 1 ), e.g. it can be at an absolute pressure lying in the range 0.2 MPa to 1.0 MPa, and preferably in the range 0.2 MPa to 0.6 MPa.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
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  • Chemical Kinetics & Catalysis (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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US11/254,561 1999-07-07 2005-10-20 Method and apparatus for steam cracking hydrocarbons Expired - Fee Related US7288690B2 (en)

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US11/254,561 US7288690B2 (en) 1999-07-07 2005-10-20 Method and apparatus for steam cracking hydrocarbons

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
FR9909039A FR2796078B1 (fr) 1999-07-07 1999-07-07 Procede et dispositif de vapocraquage d'hydrocarbures
FR99/09039 1999-07-07
PCT/FR2000/001852 WO2001004236A1 (fr) 1999-07-07 2000-06-30 Procede et dispositif de vapocraquage d'hydrocarbures
US993902A 2002-02-28 2002-02-28
US11/254,561 US7288690B2 (en) 1999-07-07 2005-10-20 Method and apparatus for steam cracking hydrocarbons

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US10009939 Continuation 2000-06-30
PCT/FR2000/001852 Continuation WO2001004236A1 (fr) 1999-07-07 2000-06-30 Procede et dispositif de vapocraquage d'hydrocarbures
US993902A Continuation 1999-07-07 2002-02-28

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US (1) US7288690B2 (de)
EP (1) EP1192236B1 (de)
JP (1) JP4585729B2 (de)
CN (1) CN1223652C (de)
AT (1) ATE236234T1 (de)
AU (1) AU5993400A (de)
CA (1) CA2377770C (de)
DE (1) DE60001946T2 (de)
ES (1) ES2194754T3 (de)
FR (1) FR2796078B1 (de)
WO (1) WO2001004236A1 (de)

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US9434612B2 (en) 2012-11-30 2016-09-06 Elwha, Llc Systems and methods for producing hydrogen gas
US20200024525A1 (en) * 2016-01-20 2020-01-23 Sabic Global Technologies B.V. Methods and systems for superheating dilution steam and generating electricity
WO2020150244A1 (en) * 2019-01-15 2020-07-23 Sabic Global Technologies, B.V. Use of renewable energy in olefin synthesis
US10793780B2 (en) 2017-10-12 2020-10-06 Red Leaf Resources, Inc. Heating materials through co-generation of heat and electricity
WO2020245016A1 (de) 2019-06-05 2020-12-10 Basf Se Elektrisch beheizte, hybride hochtemperaturverfahren
WO2022094455A1 (en) * 2020-11-02 2022-05-05 Lummus Technology Llc Electric furnace to produce olefins
WO2022200256A1 (en) 2021-03-24 2022-09-29 Sabic Global Technologies B.V. Systems and methods for olefin production in electrically-heated cracking furnace
WO2023062165A1 (en) 2021-10-14 2023-04-20 Technip Energies France Sas Ethylene plant, comprising an electrically-powered pyrolysis reactor and a feed-effluent heat exchanger
WO2024126074A1 (en) 2022-12-15 2024-06-20 Ineos Europe Ag Cracking method
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WO2024126071A1 (en) 2022-12-15 2024-06-20 Ineos Europe Ag Cracking method
RU2826998C2 (ru) * 2019-01-15 2024-09-19 Сабик Глоубл Текнолоджиз, Б.В. Применение возобновляемой энергии в синтезе олефинов
US20240424424A1 (en) * 2021-07-02 2024-12-26 Sabic Global Technologies B.V. Systems and methods for vaporizing hydrocarbon feeds

Families Citing this family (60)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB0204140D0 (en) 2002-02-22 2002-04-10 Bp Chem Int Ltd Production of olefins
RU2298027C2 (ru) * 2005-05-24 2007-04-27 Николай Геннадьевич Шляхтин Способ фракционирования углеводородного сырья и установка для его осуществления
US7789658B2 (en) * 2006-12-14 2010-09-07 Uop Llc Fired heater
WO2008076610A1 (en) * 2006-12-14 2008-06-26 Uop Llc Fired heater
US20080145805A1 (en) * 2006-12-14 2008-06-19 Towler Gavin P Process of Using a Fired Heater
US20080152549A1 (en) * 2006-12-21 2008-06-26 Towler Gavin P Preheating process for FCC regenerator
US7932204B2 (en) * 2007-12-21 2011-04-26 Uop Llc Method of regenerating catalyst in a fluidized catalytic cracking unit
US7811446B2 (en) * 2007-12-21 2010-10-12 Uop Llc Method of recovering energy from a fluid catalytic cracking unit for overall carbon dioxide reduction
US7935245B2 (en) * 2007-12-21 2011-05-03 Uop Llc System and method of increasing synthesis gas yield in a fluid catalytic cracking unit
US9062525B2 (en) * 2011-07-07 2015-06-23 Single Buoy Moorings, Inc. Offshore heavy oil production
RU2478688C2 (ru) * 2011-12-20 2013-04-10 Закрытое акционерное общество Научно-проектное производственно-строительное объединение "Грантстрой" (ЗАО НППСО "Грантстрой") Многостадийный способ получения водородосодержащего газообразного топлива и теплогазогенераторная установка его реализации (способ аракеляна г.г.)
US9249019B2 (en) 2012-12-09 2016-02-02 Zakritoe akzionernoe obshestvo Nauchno-proektnoe prozvodstvenno-stroitelnoe obedinenie “GRANDSTROY” Multistage method for producing hydrogen-containing gaseous fuel and thermal gas-generator setup of its implementation
GB2514934B (en) * 2012-01-20 2019-06-05 Single Buoy Moorings Incorporated Offshore heavy oil production
US20140058161A1 (en) * 2012-08-21 2014-02-27 Uop Llc Methane conversion apparatus and process with improved mixing using a supersonic flow reactor
EP3056481A1 (de) * 2015-02-16 2016-08-17 Linde Aktiengesellschaft Verfahren und Anlage zur Herstellung von Kohlenwasserstoffen
CN106552564A (zh) * 2015-09-30 2017-04-05 中国石油化工股份有限公司 超声波管式热裂解系统及应用该系统的热裂解工艺
DE102016209172A1 (de) * 2016-05-25 2017-11-30 Linde Aktiengesellschaft Emissionsreduziertes Verfahren zur Herstellung von Olefinen
EP3249028A1 (de) * 2016-05-25 2017-11-29 Linde Aktiengesellschaft Emissionsreduziertes verfahren zur herstellung von olefinen
CN107189854B (zh) * 2017-05-28 2023-10-31 天津大学 蒸汽再压缩和热量交换集成的微藻油脂萃取系统
EP3724298A1 (de) * 2017-12-15 2020-10-21 SABIC Global Technologies B.V. Verfahren zur vorwärmung von naphtha in katalytischen naphtha-krackverfahren
EP3574991A1 (de) 2018-05-31 2019-12-04 Haldor Topsøe A/S Durch widerstandsheizung erhitzte dampfreformierung
PT3801871T (pt) 2018-05-31 2026-05-12 Topsoe As Reaes endotrmicas aquecidas por aquecimento por resistncia
AR115968A1 (es) 2018-08-31 2021-03-17 Dow Global Technologies Llc Sistemas y procesos para perfeccionar la mejora de hidrocarburos
AR115971A1 (es) 2018-08-31 2021-03-17 Dow Global Technologies Llc Sistemas y procesos para tratar térmicamente una corriente que contiene hidrocarburos
AR115969A1 (es) 2018-08-31 2021-03-17 Dow Global Technologies Llc Sistemas y procesos para transferir calor mediante sal fundida durante la mejora de hidrocarburos
EP3953296A1 (de) 2019-04-08 2022-02-16 Haldor Topsøe A/S Anlage für chemische synthese
EP3725865A1 (de) * 2019-04-17 2020-10-21 SABIC Global Technologies B.V. Verwendung von erneuerbarer energie in der olefinsynthese
EP3730592A1 (de) * 2019-04-24 2020-10-28 SABIC Global Technologies B.V. Verwendung von erneuerbarer energie bei der olefinsynthese
CA3155515A1 (en) 2019-10-01 2021-04-08 Haldor Topsoe A/S On demand hydrogen from methanol
KR102968670B1 (ko) 2019-10-01 2026-05-27 토프쉐 에이/에스 맞춤형 합성 가스
WO2021063796A1 (en) 2019-10-01 2021-04-08 Haldor Topsøe A/S On demand synthesis gas from methanol
EP4038013A1 (de) 2019-10-01 2022-08-10 Haldor Topsøe A/S Wasserstoff aus ammoniak auf anfrage
DK4037821T3 (da) 2019-10-01 2023-09-04 Topsoe As Offshore-reforminginstallation eller -fartøj
JP7662621B2 (ja) 2019-10-01 2025-04-15 トプソー・アクチエゼルスカベット シアン化物オンデマンド
WO2021094346A1 (en) * 2019-11-12 2021-05-20 Haldor Topsøe A/S Electric steam cracker
CA3163958C (en) 2019-12-09 2025-05-13 Coolbrook Oy HEAT INTEGRATION INTO A HYDROCARBON PROCESSING PLANT
EP4103667A1 (de) 2020-02-14 2022-12-21 SABIC Global Technologies B.V. Energieeffizientes dampfcrackverfahren
CN113307716B (zh) * 2020-02-26 2023-05-05 中国石油化工股份有限公司 生产乙炔和炭黑的方法、生产乙炔和合成气的方法及系统
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WO2022008052A1 (en) * 2020-07-09 2022-01-13 Basf Antwerpen N.V. Method for steam cracking
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WO2023287602A1 (en) * 2021-07-15 2023-01-19 Exxonmobil Chemical Patents Inc. Steam cracking with supplemental electrical heating
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KR102690040B1 (ko) * 2023-05-04 2024-07-29 주식회사 한국가스기술공사 그린수소 생성이 가능한 메탄 열분해 반응장치
WO2025252545A1 (en) 2024-06-07 2025-12-11 Basf Se Energy efficiency in chemical processes

Citations (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3765167A (en) * 1972-03-06 1973-10-16 Metallgesellschaft Ag Power plant process
US3819740A (en) 1970-09-03 1974-06-25 Kureha Chemical Ind Co Ltd Process for thermally cracking hydrocarbons
US3862898A (en) * 1973-07-30 1975-01-28 Pullman Inc Process for the production of olefinically unsaturated hydrocarbons
US4287377A (en) 1978-08-07 1981-09-01 Imperial Chemical Industries Limited Hydrocarbon conversion
US4479355A (en) 1983-02-25 1984-10-30 Exxon Research & Engineering Co. Power plant integrating coal-fired steam boiler with air turbine
EP0252356A1 (de) 1986-06-25 1988-01-13 Naphtachimie S.A. Verfahren und Ofen für das Dampfkracken von Kohlenwasserstoffen für die Zubereitung von Olefinen und Diolefinen
EP0252355A1 (de) 1986-06-25 1988-01-13 Naphtachimie S.A. Verfahren und Ofen für das Dampfkracken von Kohlenwasserstoffen für die Zubereitung von Olefinen und Diolefinen
US4777318A (en) 1986-06-25 1988-10-11 Naphthachimie Process and furnace for the steam cracking of hydrocarbons for the preparation of olefins and diolefins
US4912282A (en) * 1983-04-19 1990-03-27 Linde Aktiengesellschaft Process for operating a plant for the cracking of hydrocarbons
WO1992011931A1 (fr) 1990-12-28 1992-07-23 Naphtachimie S.A. Procede de fabrication de produits chimiques
EP0733609A1 (de) 1995-03-23 1996-09-25 Institut Francais Du Petrole Verfahren zur thermischen Umsetzung von aliphatischen gesättigten oder ungesättigten Kohlenwasserstoffen in acetylenischen Kohlenwasserstoffen
JPH09235564A (ja) 1996-02-27 1997-09-09 Jgc Corp 炭化水素の熱分解方法および熱分解設備
EP0806467A1 (de) 1996-05-06 1997-11-12 Institut Français du Pétrole Verfahren und Einrichtung zur thermischen Umsetzung von Kohlenwasserstoffen zu ungesättigten aliphatischen Kohlenwasserstoffen durch Kombination einer Dampfkrackung und einer Pyrolysestufe
US6734331B2 (en) * 1996-12-23 2004-05-11 Egt Developments, Llc Process for producing olefins and diolefins
US6958363B2 (en) * 2003-03-15 2005-10-25 Conocophillips Company Hydrogen use in a GTL plant

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4617109A (en) * 1985-12-23 1986-10-14 The M. W. Kellogg Company Combustion air preheating

Patent Citations (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3819740A (en) 1970-09-03 1974-06-25 Kureha Chemical Ind Co Ltd Process for thermally cracking hydrocarbons
US3765167A (en) * 1972-03-06 1973-10-16 Metallgesellschaft Ag Power plant process
US3862898A (en) * 1973-07-30 1975-01-28 Pullman Inc Process for the production of olefinically unsaturated hydrocarbons
US4287377A (en) 1978-08-07 1981-09-01 Imperial Chemical Industries Limited Hydrocarbon conversion
US4479355A (en) 1983-02-25 1984-10-30 Exxon Research & Engineering Co. Power plant integrating coal-fired steam boiler with air turbine
US4912282A (en) * 1983-04-19 1990-03-27 Linde Aktiengesellschaft Process for operating a plant for the cracking of hydrocarbons
US4777318A (en) 1986-06-25 1988-10-11 Naphthachimie Process and furnace for the steam cracking of hydrocarbons for the preparation of olefins and diolefins
US4762958A (en) 1986-06-25 1988-08-09 Naphtachimie S.A. Process and furnace for the steam cracking of hydrocarbons for the preparation of olefins and diolefins
EP0252355A1 (de) 1986-06-25 1988-01-13 Naphtachimie S.A. Verfahren und Ofen für das Dampfkracken von Kohlenwasserstoffen für die Zubereitung von Olefinen und Diolefinen
EP0252356A1 (de) 1986-06-25 1988-01-13 Naphtachimie S.A. Verfahren und Ofen für das Dampfkracken von Kohlenwasserstoffen für die Zubereitung von Olefinen und Diolefinen
WO1992011931A1 (fr) 1990-12-28 1992-07-23 Naphtachimie S.A. Procede de fabrication de produits chimiques
EP0733609A1 (de) 1995-03-23 1996-09-25 Institut Francais Du Petrole Verfahren zur thermischen Umsetzung von aliphatischen gesättigten oder ungesättigten Kohlenwasserstoffen in acetylenischen Kohlenwasserstoffen
JPH09235564A (ja) 1996-02-27 1997-09-09 Jgc Corp 炭化水素の熱分解方法および熱分解設備
EP0806467A1 (de) 1996-05-06 1997-11-12 Institut Français du Pétrole Verfahren und Einrichtung zur thermischen Umsetzung von Kohlenwasserstoffen zu ungesättigten aliphatischen Kohlenwasserstoffen durch Kombination einer Dampfkrackung und einer Pyrolysestufe
US6734331B2 (en) * 1996-12-23 2004-05-11 Egt Developments, Llc Process for producing olefins and diolefins
US6958363B2 (en) * 2003-03-15 2005-10-25 Conocophillips Company Hydrogen use in a GTL plant

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Patent Abstracts of Japan of JP 9-235564 dated Sep. 9, 1997.

Cited By (40)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7799288B2 (en) * 2007-06-29 2010-09-21 Uop Llc Apparatus for recovering power from FCC product
WO2013025570A1 (en) 2011-08-12 2013-02-21 Harris Corporation Processing device an method for treating hydrocarbon feedstock using radio frequency waves
US10000709B2 (en) 2011-08-12 2018-06-19 Harris Corporation Hydrocarbon resource processing device including radio frequency applicator and related methods
US9376634B2 (en) 2011-08-12 2016-06-28 Harris Corporation Hydrocarbon resource processing device including radio frequency applicator and related methods
US8932435B2 (en) 2011-08-12 2015-01-13 Harris Corporation Hydrocarbon resource processing device including radio frequency applicator and related methods
US8960285B2 (en) 2011-11-01 2015-02-24 Harris Corporation Method of processing a hydrocarbon resource including supplying RF energy using an extended well portion
WO2013066579A2 (en) 2011-11-01 2013-05-10 Harris Corporation Method of processing a hydrocarbon resource including supplying rf energy using an extended well portion
WO2013106384A1 (en) 2012-01-13 2013-07-18 Harris Corporation Hydrocarbon resource processing apparatus including a load resonance tracking circuit and related methods
WO2013106422A2 (en) 2012-01-13 2013-07-18 Harris Corporation Hydrocarbon resource processing device including spirally wound electrical conductors and related methods
US8771481B2 (en) 2012-01-13 2014-07-08 Harris Corporation Hydrocarbon resource processing apparatus including a load resonance tracking circuit and related methods
US8840780B2 (en) 2012-01-13 2014-09-23 Harris Corporation Hydrocarbon resource processing device including spirally wound electrical conductors and related methods
US8858785B2 (en) 2012-01-13 2014-10-14 Harris Corporation Hydrocarbon resource processing device including spirally wound electrical conductor and related methods
WO2013142543A2 (en) 2012-03-21 2013-09-26 Harris Corporation Method for forming a hydrobarbon resource rf radiator
US8960291B2 (en) 2012-03-21 2015-02-24 Harris Corporation Method for forming a hydrocarbon resource RF radiator
US8726986B2 (en) 2012-04-19 2014-05-20 Harris Corporation Method of heating a hydrocarbon resource including lowering a settable frequency based upon impedance
WO2013158548A1 (en) 2012-04-19 2013-10-24 Harris Corporation Method of heating a hydrocarbon resource including lowering a settable frequency based upon impedance
US9140099B2 (en) 2012-11-13 2015-09-22 Harris Corporation Hydrocarbon resource heating device including superconductive material RF antenna and related methods
US9156688B2 (en) 2012-11-30 2015-10-13 Elwha Llc Systems and methods for producing hydrogen gas
US9434612B2 (en) 2012-11-30 2016-09-06 Elwha, Llc Systems and methods for producing hydrogen gas
US20200024525A1 (en) * 2016-01-20 2020-01-23 Sabic Global Technologies B.V. Methods and systems for superheating dilution steam and generating electricity
US10793780B2 (en) 2017-10-12 2020-10-06 Red Leaf Resources, Inc. Heating materials through co-generation of heat and electricity
WO2020150244A1 (en) * 2019-01-15 2020-07-23 Sabic Global Technologies, B.V. Use of renewable energy in olefin synthesis
US12065398B2 (en) 2019-01-15 2024-08-20 Sabic Global Technologies B.V. Use of renewable energy in methanol synthesis
CN113966380A (zh) * 2019-01-15 2022-01-21 沙特基础工业全球技术公司 可再生能量在烯烃合成中的使用
US20220127209A1 (en) * 2019-01-15 2022-04-28 Sabic Global Technologies B.V. Use of renewable energy in olefin synthesis
WO2020150249A1 (en) 2019-01-15 2020-07-23 Sabic Global Technologies, B.V. Use of intermittent energy in the production of chemicals
US12678760B2 (en) 2019-01-15 2026-07-14 Sabic Global Technologies B.V. Use of renewable energy in methanol synthesis
US12186726B2 (en) 2019-01-15 2025-01-07 Sabic Global Technologies B.V. Use of renewable energy in the production of chemicals
US12128378B2 (en) * 2019-01-15 2024-10-29 Sabic Global Technologies B.V. Use of renewable energy in olefin synthesis
RU2826998C2 (ru) * 2019-01-15 2024-09-19 Сабик Глоубл Текнолоджиз, Б.В. Применение возобновляемой энергии в синтезе олефинов
WO2020245016A1 (de) 2019-06-05 2020-12-10 Basf Se Elektrisch beheizte, hybride hochtemperaturverfahren
US12334741B2 (en) 2019-06-05 2025-06-17 Basf Se Electrically heated, hybrid high-temperature method
WO2022094455A1 (en) * 2020-11-02 2022-05-05 Lummus Technology Llc Electric furnace to produce olefins
WO2022200256A1 (en) 2021-03-24 2022-09-29 Sabic Global Technologies B.V. Systems and methods for olefin production in electrically-heated cracking furnace
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WO2023062165A1 (en) 2021-10-14 2023-04-20 Technip Energies France Sas Ethylene plant, comprising an electrically-powered pyrolysis reactor and a feed-effluent heat exchanger
WO2024126071A1 (en) 2022-12-15 2024-06-20 Ineos Europe Ag Cracking method
WO2024126078A1 (en) 2022-12-15 2024-06-20 Ineos Europe Ag Method for cracking hydrocarbons
WO2024126074A1 (en) 2022-12-15 2024-06-20 Ineos Europe Ag Cracking method

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